US4237619A - Fluidized bed apparatus - Google Patents

Fluidized bed apparatus Download PDF

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Publication number
US4237619A
US4237619A US05/970,069 US97006978A US4237619A US 4237619 A US4237619 A US 4237619A US 97006978 A US97006978 A US 97006978A US 4237619 A US4237619 A US 4237619A
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Prior art keywords
fluidized
leg
starch
zone
chamber
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Expired - Lifetime
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US05/970,069
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English (en)
Inventor
Willard E. Ledding
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Unilever Bestfoods North America
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Unilever Bestfoods North America
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Filing date
Publication date
Application filed by Unilever Bestfoods North America filed Critical Unilever Bestfoods North America
Priority to US05/970,069 priority Critical patent/US4237619A/en
Priority to CA341,052A priority patent/CA1124058A/en
Priority to AU53480/79A priority patent/AU533243B2/en
Priority to AR279205A priority patent/AR223357A1/es
Priority to BR7908087A priority patent/BR7908087A/pt
Priority to MX180504A priority patent/MX152372A/es
Priority to IN1302/CAL/79A priority patent/IN152101B/en
Priority to JP16221079A priority patent/JPS5581739A/ja
Priority to US06/136,131 priority patent/US4266348A/en
Application granted granted Critical
Publication of US4237619A publication Critical patent/US4237619A/en
Anticipated expiration legal-status Critical
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
    • F26B3/092—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed agitating the fluidised bed, e.g. by vibrating or pulsating
    • F26B3/0923—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed agitating the fluidised bed, e.g. by vibrating or pulsating by mechanical means, e.g. vibrated plate, stirrer

Definitions

  • This invention relates to fluidization, and more particularly to apparatus and process for carrying out fluidized bed operations.
  • Fluidized beds have been used for many years in the chemical industry for carrying out a wide variety of chemical reactions and/or unit operations.
  • One of the primary advantages of fluidized bed systems arises from the fact that the high turbulence created in the bed provides high heat transfer characteristics as well as complete mixing of the solids and gases within the bed itself.
  • the fluidized bed system utilized in those two patents comprises three distinct fluidized zones, an upper and lower fluidized zone, each of which is provided with paddle-type agitators to promote more complete mixing.
  • Each of the upper and lower fluidized zones communicates each with the other by means of a plurality of tubular zones surrounded by heat transfer media whereby most, if not all, of the heat transfer to or from the fluidized bed is passed through the walls of the tubular fluidized zones.
  • the present invention is an improvement over the process and apparatus described in the foregoing patents, including improved means to discharge fluidized solids from the reactor and an improved process for use of the equipment in the drying of starch.
  • the present invention is directed to fluidization of solid materials, particularly solid particulate materials which have a tendency to adhere to agglomerate.
  • Apparatus of the present invention is useful in chemical and/or physical processes in which such particulate materials are fluidized and subjected to heat transfer during fluidization, usually to supply heat to the particulate material.
  • the improved apparatus includes a fluidization system comprising an upper agitated fluidized zone and a lower agitated fluidized zone with an intermediate fluidized zone formed of a plurality of tubular zones communicating with each of the upper and lower fluidizing zones whereby fluidizing gas is passed upwardly through the lower agitated fluidized zone, through the intermediate zone and into the upper agitated fluidized zone to fluidize the solids in each of the three zones.
  • a discharge means comprising a substantially vertical fluidized zone or leg substantially parallel to the foregoing three zones, including means for supplying a fluidizing medium near the base and means for removing fluidized solids at a level above the base of the parallel zone.
  • fluidized solids are transported from the upper or lower fluidized zones, preferably the former, to the discharge leg in which they are fluidized by means of the fluidizing gas supplied at the base thereof.
  • Solid particulate matter is removed from outlet means provided in the leg, the outlet means being repositionable, if desired, to establish the level of fluidized solids in the upper fluidized zone.
  • the discharge system of the invention has the further advantage in that it can be positioned at a level which can determine the level of fluidized solids in the upper agitated fluidized zone.
  • the discharge leg can be operated at levels different from the level of fluidized solids in the upper fluidized zone.
  • the flow of fluidizing gas into the discharge leg can be varied so that, for a given height of solids in the upper fluidized zone, any desired height in the discharge leg can be achieved by control of fluidizing gas to the leg.
  • a process for utilizing apparatus of the type described in the drying of starch where starch supplied to the fluidized system described above is controlled so as to have a moisture content not exceeding twenty-seven percent moisture by weight, the fluidized bed system can be operated at higher temperatures and exit-gas wet-bulb temperatures without appreciably damaging the starch. It is therefore preferred, when processing starch produced from wet milling, in the form of a centrifuge-cake having a moisture content ranging from about twenty-eight to forty-five percent by weight, to recycle dried starch for blending with the centrifuge-cake starch. The amount of the recycled, dry starch (having a moisture content below nineteen percent by weight) is adjusted so that the total moisture content of the starch supplied to the fluidized bed dryer does not exceed twenty-seven percent by weight.
  • FIG. 1 is a sectional view of a fluidized bed reactor suitable for use in the process of the invention.
  • FIG. 2 is a view in elevation of the fluidized bed system illustrated in FIG. 1, equipped with an airlift-leg discharge system.
  • FIG. 3 is a view in elevation of the fluidized bed system illustrated in FIG. 1, equipped with an alternative airlift-leg discharge system.
  • FIG. 1 of the drawings there is shown a fluidized bed system of the type described in those patents including an upper fluidized zone 10 having an axially-extending agitator shaft positioned therein. Mounted on the shaft 12 are a plurality of agitator blades 14 to facilitate mixing within the upper fluidized zone 10. Also provided in the upper fluidized zone is an inlet supply port 16 through which the material to be fluidized is supplied.
  • a lower fluidized zone 18 Positioned below the upper fluidized zone 10 is a lower fluidized zone 18, also equipped with an agitator shaft 20 and a plurality of mechanical agitators 22 mounted therein to permit mixing within the lower fluidized zone 18.
  • the agitators in both the upper and lower fluidized zones 10 and 18 are driven by suitable motors or like driving means, not illustrated in the drawing.
  • the intermediate or tubular fluidized zones 24 are preferably equipped with a jacket 26 surrounding the tubes 24 so that a suitable heat exchange medium such as steam can be supplied to the inlet port 30 and the discharge port 28 to supply heat (or to remove it) from the tubular zones 24.
  • a suitable heat exchange medium such as steam
  • the tubular zones 24 have a cross-sectional area which is significantly smaller than the cross-sectional area of either the upper or lower fluidized zones 10 or 18, respectively. Fluidizing air is thus supplied to the lower fluidizing zone 18 by means of a suitable inlet port 32 in accordance with any of a variety of techniques known to the art.
  • the solid particulate matter to be fluidized is introduced, preferably at the supply port 16 and fluidizing gas is supplied to the inlet port 32 in the lower fluidizing zone 18.
  • the fluidizing gas supplied to the lower fluidizing zone 18 thus serves to fluidize the solids present in the lower fluidized zone 18, the tubular zones 24 and the upper fluidized zone 10.
  • the fluidizing gas is thus removed from a port 34 near the top of the upper fluidized zone 10 for passage to a cyclone separator or the like in accordance with conventional techniques.
  • the fluidized solids can be, where desired, removed, in the embodiment shown in FIG. 1, through a discharge port 36 communicating with the interior of the lower fluidized zone 18.
  • FIG. 2 illustrates the improved airlift-leg discharge system from one concept of this invention, the fluidized bed system of FIG. 2 being the same as that shown in FIG. 1 including the upper fluidizing zone 10, the lower fluidized zone 18, and the jacket 26 enclosing the intermediate tubular zone (the tubular zones 24 are not visible in FIG. 2) by the discharge means includes an elongate tubular fluidized zone 38 which extends vertically, substantially parallel, to the upper and lower fluidized zones 10 and 18 as well as the intermediate tubular fluidized zones 24.
  • the airlift discharge leg 38 communicates with the discharge port 36, and at its upper end, communicates with the fluidizing gas exhaust port 34.
  • the discharge port 36 includes a plenum chamber 42 to which a fluidizing gas, such as air, is supplied.
  • the airlift discharge leg also includes an adjustable discharge port 44, the level of which can be varied depending on the system to be fluidized.
  • a section of the airleg discharge tube 38 is provided with a plurality of collars 46, 48 and 50, one of which (collar 50) carries the discharge port 44.
  • the collars 46 and 50 can be removed and their position reversed so that the collar 50, carrying the discharge port 44, is positioned at a level above the collar 46.
  • the relative positions of collars 50 and 48 are simply reversed so that the discharge port 44 is positioned at a level lower than that shown in FIG. 2.
  • fluidizing gas is supplied to the plenum chamber 42 only or to the plenum chamber and the fluidizing gas inlet port 32 simultaneously.
  • the fluidizing gas thus supplied serves to fluidize the solids in both the upper and lower zones 10 and 18 as well as the intermediate tubular fluidized zones 24 and the airlift discharge leg 38.
  • the solids to be fluidized are supplied to the inlet supply port 16 and are fluidized within the upper fluidized zone 10, the intermediate tubular fluidized zones 24, and the lower fluidized zone 18, from which they pass into the discharge port 36.
  • the particulate solids which are passed downwardly through the fluidized bed system pass through the discharge port 36, but are lifted, by means of the fluidizing gas supplied to the plenum chamber 42, into the airleg discharge tube 38 where a solids level is established corresponding to that in the fluidized zone 10.
  • the particulate solids which may be above the level of the fluidized bed in the upper fluidized zone 10 are passed downwardly through the discharge port 44 for recovery.
  • the elevation of the discharge port 44 on the airlift leg discharge tube 38 in combination with the flow rate of the fluidizing gas in the leg 38 determines the level of fluidized solids in the upper fluidized zone 10.
  • Fluidizing gas passing through the airlift leg discharge tube 38 is permitted to exit through the fluidizing gas discharge port 50 for passage to a cyclone or the like, either with or without the fluidizing gas supplied to inlet 32, the latter being discharged via exit port 34.
  • the use of the airleg discharge tube as illustrated obviates the need for a rotary airlock of the type employed by the prior art, while providing the further advantage of fixing the level of fluidized solids in the upper fluidized zone 10.
  • the discharge leg enables the product to be elevated to significant heights.
  • the upper and lower agitated zones serve to prevent channeling of the starch and hence improve efficiency in the drying operation.
  • substantially all of the heat supplied to the system is supplied by means of the heat exchange media introduced to the jacket 26 surrounding the plurality of fluidized zones, each of which have a cross-sectional area significantly less than the cross-sectional area of either the upper and lower fluidized zones.
  • the starch recovered from the dryer does undergo damage, manifesting itself as an increase in the viscosity of an alkaline slurry of the starch and by significant increases of percent gelatinized starch granules.
  • the heat supplied to the bed and the temperature of the inlet air must be reduced to give a wet-bulb temperature of the exit gases of less than about 57° C.
  • the air volume supplied to the dryer must be increased, thereby increasing energy and power costs.
  • the fluidized dryer can be operated at significantly higher temperatures such that the wet-bulb temperature of the exit gas is above about 57° C., all without damage to the starch.
  • starch having a moisture content of twenty-eight percent or more is blended with dried starch which is recycled from the fluidized bed dryer, with the amount of the dried starch being adjusted so that the moisture content of the starch blend is twenty-seven percent or less, is supplied to a fluidized bed reactor of the sort shown in either FIG. 1 or FIG. 2.
  • the dryer is then operated at a temperature such that the wet-bulb temperature of the exit gases is above 54° C., and preferably 60°-95° C. Because the moisture level of the starch is twenty-seven percent or below, the elevated temperatures used in the fluidized dryer serve to minimize operating costs while increasing dryer capacity without any significant damage to the starch.
  • the starch to be dried is a cake obtained from centrifuging in the conventional starch wet milling process, and contains from about twenty-eight to forty-five percent moisture by weight. That wet starch is thus blended with starch obtained as produced from the dryer by way of a recycle of a portion of the dried starch product.
  • the dried starch recovered as produced from the dryer generally has a moisture content ranging from about two to nineteen percent moisture by weight, depending somewhat on the desired use for the dried starch.
  • the dried starch can be removed from the discharge port 36, and a portion recovered from line 54. Another portion is recycled via line 56 for passage to a blender 58 to which centrifuge cake is supplied by line 60 to make up the supply of starch having a moisture content of twenty-seven percent or below.
  • the improved drying process described above can be carried out in apparatus other than that described in FIGS. 1 and 2.
  • the starch may be dried using the principles of the process of this invention in a conventional fluidized bed dryer, although such conventional dryers are not as effective by reason of the channeling phenomenon and the difficulty in fluidizing the wet starch.
  • This example illustrates the use of a fluidized bed dryer having the configuration shown in FIG. 2 of the drawing in the drying of starch.
  • test L utilized a starch having a moisture content of 27% or below.
  • the condition of the starch, from the standpoint of damage, is measured by the alkali sensitivity test in which a solution of 150 ml of 1% by weight sodium hydroxide solution in 50 ml of distilled water is stirred vigorously with an electric stirrer. Then 88 g dry basis of starch is added in 5 to 6 seconds to the vortex of the stirred solution. Stirring is continued for 5 minutes.
  • the viscosity of the solution is measured immediately using a Brookfield viscometer, models RVT or RVF with a No. 1 spindle at 20 rpm. The reading in centipoises (cp) is taken after running the viscometer for 20 seconds.
  • an air inlet tube 52 to inject air into one or more of the tubular zones 24. Without limiting this embodiment as to theory, it is believed that the air injection tube 52 serves to transport a greater volume of hot dried starch from the tubular zones 24 to the upper fluidized zones 10 to facilitate the overall drying operation.
  • FIG. 3 of the drawing illustrates a modified airlift discharge system.
  • starch having somewhat higher moisture contents (e.g., above about 12% moisture by weight)
  • starch having somewhat higher moisture contents (e.g., above about 12% moisture by weight)
  • the airlift leg discharge system is otherwise the same and operates in the same manner. The only major difference is that the discharge port 36' permits the flow of starch from the upper fluidized zone 10 to the lower portion of the discharge leg 38 as illustrated in FIG. 3.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Microbiology (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Drying Of Solid Materials (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
US05/970,069 1978-12-15 1978-12-15 Fluidized bed apparatus Expired - Lifetime US4237619A (en)

Priority Applications (9)

Application Number Priority Date Filing Date Title
US05/970,069 US4237619A (en) 1978-12-15 1978-12-15 Fluidized bed apparatus
CA341,052A CA1124058A (en) 1978-12-15 1979-12-03 Fluidized bed process and apparatus
AU53480/79A AU533243B2 (en) 1978-12-15 1979-12-05 Fluidised bed and its use to dry starch
AR279205A AR223357A1 (es) 1978-12-15 1979-12-07 Aparato mejorado de lecho fluidificado y procedimiento para el secado por fluidizado segun dicho aparato,particularmente para almidon
BR7908087A BR7908087A (pt) 1978-12-15 1979-12-11 Aparelho para conduzir operacao fluidizadas,e,processo para a secagem fluidizada do amido
MX180504A MX152372A (es) 1978-12-15 1979-12-13 Mejoras en aparato de lecho fluidizado para el secado de almidon
IN1302/CAL/79A IN152101B (enrdf_load_stackoverflow) 1978-12-15 1979-12-14
JP16221079A JPS5581739A (en) 1978-12-15 1979-12-15 Device for performing fluidizing operation and its fluidizing method
US06/136,131 US4266348A (en) 1978-12-15 1980-03-31 Fluidized bed process

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US05/970,069 US4237619A (en) 1978-12-15 1978-12-15 Fluidized bed apparatus

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US06/136,131 Division US4266348A (en) 1978-12-15 1980-03-31 Fluidized bed process

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US4237619A true US4237619A (en) 1980-12-09

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US05/970,069 Expired - Lifetime US4237619A (en) 1978-12-15 1978-12-15 Fluidized bed apparatus

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US (1) US4237619A (enrdf_load_stackoverflow)
JP (1) JPS5581739A (enrdf_load_stackoverflow)
AR (1) AR223357A1 (enrdf_load_stackoverflow)
AU (1) AU533243B2 (enrdf_load_stackoverflow)
BR (1) BR7908087A (enrdf_load_stackoverflow)
CA (1) CA1124058A (enrdf_load_stackoverflow)
IN (1) IN152101B (enrdf_load_stackoverflow)
MX (1) MX152372A (enrdf_load_stackoverflow)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0182295A3 (en) * 1984-11-15 1987-09-02 Cpc International Inc. Dusting powder compositions containing modified starch
NL9302094A (nl) * 1993-12-02 1995-07-03 Avebe Coop Verkoop Prod Fluidisatie van een bed van zetmeelpoeder.
US5575085A (en) * 1995-07-17 1996-11-19 Western Syncoal Company Apparatus and method for controlling the rotary airlocks in a coal processing system by reversing the motor current rotating the air lock
US6191116B1 (en) 1998-04-27 2001-02-20 National Starch And Chemical Investment Holding Corporation Highly soluble, hydratable, viscous, solution stable pyrodextrins, process of making and use thereof
US20100192401A1 (en) * 2006-06-21 2010-08-05 Klaus Stanke Process and plant for treatment of wet material

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2005263867A (ja) * 2004-03-16 2005-09-29 Oji Cornstarch Co Ltd 食物繊維高含有焙焼デキストリン及びその製造方法
JP6632960B2 (ja) * 2016-12-07 2020-01-22 オルガノフードテック株式会社 澱粉の製造方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3233336A (en) * 1962-02-26 1966-02-08 Exxon Research Engineering Co Apparatus for drying solid polymer
US3349500A (en) * 1966-03-23 1967-10-31 Dorr Oliver Inc Agglomerative drying
US3967975A (en) * 1974-11-25 1976-07-06 Cpc International Inc. Fluidization apparatus
US4021927A (en) * 1974-11-25 1977-05-10 Cpc International Inc. Process for fluidization
US4106210A (en) * 1977-01-06 1978-08-15 Dorr-Oliver Incorporated Solids discharge system with cooling means for pressurized fluid bed reactors

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DK153526B (da) * 1974-11-25 1988-07-25 Cpc International Inc Fluidiseringsfremgangsmaade, isaer til brug paa vanskeligt fluidiserbare materialer

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3233336A (en) * 1962-02-26 1966-02-08 Exxon Research Engineering Co Apparatus for drying solid polymer
US3349500A (en) * 1966-03-23 1967-10-31 Dorr Oliver Inc Agglomerative drying
US3967975A (en) * 1974-11-25 1976-07-06 Cpc International Inc. Fluidization apparatus
US4021927A (en) * 1974-11-25 1977-05-10 Cpc International Inc. Process for fluidization
US4106210A (en) * 1977-01-06 1978-08-15 Dorr-Oliver Incorporated Solids discharge system with cooling means for pressurized fluid bed reactors

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0182295A3 (en) * 1984-11-15 1987-09-02 Cpc International Inc. Dusting powder compositions containing modified starch
NL9302094A (nl) * 1993-12-02 1995-07-03 Avebe Coop Verkoop Prod Fluidisatie van een bed van zetmeelpoeder.
US5575085A (en) * 1995-07-17 1996-11-19 Western Syncoal Company Apparatus and method for controlling the rotary airlocks in a coal processing system by reversing the motor current rotating the air lock
US6191116B1 (en) 1998-04-27 2001-02-20 National Starch And Chemical Investment Holding Corporation Highly soluble, hydratable, viscous, solution stable pyrodextrins, process of making and use thereof
US20100192401A1 (en) * 2006-06-21 2010-08-05 Klaus Stanke Process and plant for treatment of wet material

Also Published As

Publication number Publication date
AU5348079A (en) 1980-06-19
AR223357A1 (es) 1981-08-14
JPS5581739A (en) 1980-06-20
JPH0113894B2 (enrdf_load_stackoverflow) 1989-03-08
BR7908087A (pt) 1980-09-09
MX152372A (es) 1985-07-09
IN152101B (enrdf_load_stackoverflow) 1983-10-15
AU533243B2 (en) 1983-11-10
CA1124058A (en) 1982-05-25

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